US20030070963A1 - Process and apparatus for cracking hydrocarbons - Google Patents
Process and apparatus for cracking hydrocarbons Download PDFInfo
- Publication number
- US20030070963A1 US20030070963A1 US10/274,987 US27498702A US2003070963A1 US 20030070963 A1 US20030070963 A1 US 20030070963A1 US 27498702 A US27498702 A US 27498702A US 2003070963 A1 US2003070963 A1 US 2003070963A1
- Authority
- US
- United States
- Prior art keywords
- catalyst
- cracking
- reaction tubes
- process according
- coating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
- C07C2523/04—Alkali metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/20—Vanadium, niobium or tantalum
- C07C2523/22—Vanadium
Definitions
- the invention relates to a process for cracking hydrocarbons, hydrocarbon mixtures or hydrocarbon fractions and an apparatus having a catalyst coating.
- thermal cracking furnaces with at least one convection zone and at least one radiant zone are used, as is known.
- thermal cracking is performed in a burner-heated radiant zone while, in the convection zone, hydrocarbons and other fluids are heated against flue gas by heat exchangers placed therein.
- hydrocarbons and process vapor are preheated in the heat exchangers of the convection zone and a hydrocarbon/vapor mixture is fed to the coils placed in the radiant zone.
- the product gases are quickly cooled in a downstream quench exchanger to interrupt the reactions.
- the cracking tubes or coils can be filled, for example for thermocatalytic cracking, at least partially with a gasification catalyst. It has been shown that catalyst fillings in conventional reaction tubes or coils of pyrolysis furnaces or steam crackers entails a series of drawbacks. Because of the catalyst fillings within the reaction tubes or coils, the pressure loss of the individual reaction tubes/coils increases considerably. Further, the inherent weight of the reaction tubes/coils filled with catalyst is clearly higher in comparison to unfilled reaction tubes/coils, thereby increasing the mechanical stress.
- Patent DE 44 00 430 A1 describes a process for thermocatalytic cracking of higher-boiling hydrocarbons and a cracking furnace, the problems occurring because of the catalyst fillings are taken into account by the use of straight reaction tubes without elbows.
- An object of the invention is to provide a process and an apparatus of the above-named types that avoid the named drawbacks and/or improve cracking processes overall and can optionally simplify them.
- it is possible to perform cracking without, or with only limited, losses of operating time due to downtimes caused by decoking, even at high levels of cracking activity. Further, problems occurring because of catalyst fillings in the cracking tubes are avoided as much as possible.
- the catalyst coating can be applied directly onto the internal surface of the reaction tubes.
- the catalyst coating can be applied on an adhesion promoter layer previously applied to the internal surface of the reaction tubes.
- the catalyst coating can be applied onto an auxiliary medium, either directly or on top of an adhesion promotion layer.
- the auxiliary medium such as, for example, a tubular shaped grid, is then placed within the reaction tube adjacent the internal surface thereof.
- the catalyst coatings according to the invention make it possible, in principle, to use all known shapes of reaction tubes for the cracking. Further, the catalyst coatings do not lead to considerable pressure loss occurring in the reaction tubes. Because the space/time yield is not changed by the coating, the process is especially attractive for use in existing units.
- the catalyst applied as a coating in accordance with the invention can promote the gasification of coke with water vapor, via the water-gas reaction to produce CO, CO 2 and H 2 , and/or promote the cracking reactions.
- Water vapor can be introduced with the hydrocarbon feed material.
- process steam is admixed with the hydrocarbon feedstream after preheating the feed and superheating the process steam. The endothermic water-gas reaction occurs according to the reaction equations
- the catalyst coating according to the invention can be applied by any known application process, preferably by thermal processes, by cold-coating processes such as, in particular, the slip process, by vapor deposition processes and/or by adhesion processes.
- Suitable thermal coating processes encompass, in particular, flame spraying, flame burst spraying, high-speed flame spraying, plasma spraying, arc spraying and molten bath spraying.
- catalyst powder is placed in an aqueous solution and laced with a bonding agent.
- the portion of bonding agent is generally below 10 wt. %, for example, about 0.1-10 wt. %, preferably 1-10 wt. %.
- the solution is applied as a suspension, for example by dipping, spraying, brushing, or the like.
- the layer, applied in this manner, is generally still subsequently treated thermally, for example, dried, baked or sintered.
- bonding agents phosphates, silicates and/or aluminates are particularly suitable.
- Such a slip coating can also be applied on a thermally sprayed (for example, by arc spraying) adhesion-promoting layer.
- the catalyst can promote gasification of coke with water vapor after the watergas reaction in CO, CO 2 and H 2 .
- the hydrogen obtained during the catalytic gasification can be used for cracking the hydrocarbons.
- the hydrogen obtained can also advantageously be available as an additional product, as is sought, for example, in production of synthesis gas.
- a catalyst based on calcium aluminate preferably with a doping of alkali vanadate, in particular potassium pyrovanadate, is used, because, on the one hand, it is excellently suited for the water-gas reaction and, on the other hand, can be applied by the application processes described above.
- Calcium aluminate catalysts can promote both the coke gasification and the hydrocarbon cracking.
- the invention can employ any of the known catalysts for coke gasification and/or hydrocarbon cracking. Suitable gasification catalysts are described, for example, in DD-243 708 A1, DD-243 647 A1 or patent application DE 44 00 430 A1.
- Catalysts comprising CaO, MgO and/or calcinated dolomites known from “Thermal and Catalytic Cracking of n-Heptane in Presence of CaO, MgO, and Calcinated Dolomites,” G. Taralas, V. Vassilatos, K. Sjoestroem and J. Delgado, The Canadian Journal of Chemical Engineering, Volume 69, December 1991, pages 1413-1419, are also suitable for catalyzing the coke gasification or the hydrocarbon cracking.
- the gasification activity of the catalyst is determined by its composition. By selection of the gasification catalyst composition, the gasification activity of the catalyst can be matched to the coking tendency of the hydrocarbon feed material.
- the gasification activity of the catalyst should be sufficient to prevent carbon and/or coke precipitation in the reaction tubes, or to limit it to an extent that does no damage.
- a high gasification activity does not lead to a reduction in yield, but rather, with high gasification activity, the amount of pyrolysis oil, i.e., the product fraction with a boiling point above about 200° C., clearly decreases.
- the quality of the feed material of the hydrocarbon fractions is usually characterized by the BMCI value (Bureau of Mines Correlation Index), which roughly corresponds to the aromatic content of the hydrocarbon feed material. Feed materials with a relatively low BMCI value can thus be especially well cracked. With the thermal cracking process according to the invention, hydrocarbon feed materials up to a BMCI value of about 60 can be economically processed.
- the BMCI value of the hydrocarbon feed-stocks is about 20-65, preferably 25-60, especially preferably 40-55.
- Mass speed has a value of preferably about 5-300 kg/s ⁇ m 2 , especially 10-200 kg/s ⁇ m 2 , especially preferably 20-120 kg/s ⁇ m 2 .
- Mass speed is the ratio of mass flow rate (i.e., the sum of the mass flow rate of hydrocarbon feed material and mass flow rate of vapor (kg/s)) to cross sectional area of the tube (m 2 ).
- the average internal surface load of the reaction tubes preferably remains at a value of about 10-120 kW/m 2 , especially 15-80 kW/m 2 .
- a heating surface load imposed on the reaction tubes large heat transfer or large heat input into the hydrocarbon/vapor mixture in the reaction tubes is ensured, without unduly stressing the reaction tubes.
- the product gasses can be quickly cooled in tubes of a cracked gas cooler or quench exchanger.
- the tubes of the cracked gas cooler or quench exchanger and/or other surfaces therein can be provided with a catalyst coating as described above.
- a catalyst coating as described above.
- coking is prevented or considerably limited.
- the catalyst coating according to the invention can be used in a simple way for retrofitting existing cracking units. Existing cracking units can be effectively improved by subsequently applying the catalyst coating.
- the invention further relates to a cracking furnace for cracking hydrocarbons or hydrocarbon mixtures in reaction tubes, whose reaction tubes are coated with a catalyst according to the invention.
- the invention further relates to a steam reformer with reaction tubes, whose reaction tubes are coated with a catalyst according to the invention.
- the invention finally relates to an apparatus, in particular a cracking furnace, a steam reformer, a reactor, a quench exchanger, an evaporator and/or a heat exchanger having surfaces that come into contact with carbon and/or carbon compounds, in particular hydrocarbons, during operation thereof, wherein these surfaces, in particular tube and/or wall surfaces, are coated at least partially with a catalyst in accordance with the invention, to reduce or avoid coke deposits and to promote gasification of coke and/or to promote cracking reactions.
- a catalyst in accordance with the invention, to reduce or avoid coke deposits and to promote gasification of coke and/or to promote cracking reactions.
- Such an apparatus exhibits, because of the now eliminated or at least considerably reduced production downtimes, increased unit capacity.
- the necessary maintenance expense for the apparatus can be reduced.
- the coating can be applied directly to the reaction tubes or surfaces or on top of an adhesion promoter previously applied to the reaction tube or surfaces and/or applied onto an auxiliary medium placed within the reaction tubes or on the surfaces.
- the auxiliary medium can be a grid that is preferably preshaped in the form of a tube.
- the auxiliary media here are positioned in the reaction tubes adjacent their internal surfaces.
- the coating is applied especially easily and lastingly, when the surfaces, reaction tubes and/or auxiliary media are coated by a thermal coating process, a cold coating process (particularly a slip coating process) a vapor-deposition coating process and/or an adhesive coating process.
- the catalyst coating is applied to an adhesion-promoting layer.
- the catalyst coating can be made from any catalyst that is known to promote the water-gas reaction and/or the cracking reaction.
- Catalysts comprising CaO, MgO, and/or calcinated dolomites, which promote the watergas reaction, are known, for example, from “Thermal and Catalytic Cracking of n-Heptane in Presence of CaO, MgO, and Calcinated Dolomites,” G. Taralas, V. Vassilatos, K. Sjoestroem and J. Delgado, The Canadian Journal of Chemical Engineering, Volume 69, December 1991, pages 1413 to 1419.
- Especially suitable as a catalyst coating is the above-described coating made of a catalyst based on calcium aluminate, preferably with a doping of alkali vanadate, particularly potassium pyrovanadate.
- FIG. 1 illustrates a cracking furnace with a convection zone and radiant zone
- FIG. 2 illustrates coke gasification in a reaction tube in accordance with the invention.
- FIG. 1 illustrates a typical cracking furnace showing a convection zone, radiant zone, quench exchanger and steam drum.
- the reaction tube is a catalyst coated reaction coil.
- a cracking or radiant coil has generally the shape of a meandering tube. See “Modern Furnace Design for Steam Crackers,” FIG. 2, page 10, which shows some typical examples of such coils.
- FIG. 2 illustrates coke gasification at the surface of a reaction tube coated with catalyst in accordance with the invention.
- the coke is gasified with water vapor in the presence of the catalyst in accordance with equation (1) to form CO and H 2 .
- the CO reacts with water vapor to form CO 2 and H 2 .
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/274,987 US20030070963A1 (en) | 1995-02-17 | 2002-10-22 | Process and apparatus for cracking hydrocarbons |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19505455.5 | 1995-02-17 | ||
DE19505455 | 1995-02-17 | ||
DE19600684.8 | 1996-01-10 | ||
DE19600684A DE19600684A1 (de) | 1995-02-17 | 1996-01-10 | Verfahren zum Spalten von Kohlenwasserstoffen und Vorrichtung |
US60348596A | 1996-02-20 | 1996-02-20 | |
US10/274,987 US20030070963A1 (en) | 1995-02-17 | 2002-10-22 | Process and apparatus for cracking hydrocarbons |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US60348596A Continuation | 1995-02-17 | 1996-02-20 |
Publications (1)
Publication Number | Publication Date |
---|---|
US20030070963A1 true US20030070963A1 (en) | 2003-04-17 |
Family
ID=7754289
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/274,987 Abandoned US20030070963A1 (en) | 1995-02-17 | 2002-10-22 | Process and apparatus for cracking hydrocarbons |
Country Status (3)
Country | Link |
---|---|
US (1) | US20030070963A1 (de) |
AR (1) | AR000827A1 (de) |
DE (2) | DE19600684A1 (de) |
Cited By (48)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040004028A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Converting mist flow to annular flow in thermal cracking application |
US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
US20050133417A1 (en) * | 2003-12-19 | 2005-06-23 | Bhan Opinder K. | Systems, methods, and catalysts for producing a crude product |
US20050135997A1 (en) * | 2003-12-19 | 2005-06-23 | Wellington Scott L. | Systems and methods of producing a crude product |
US20050150816A1 (en) * | 2004-01-09 | 2005-07-14 | Les Gaston | Bituminous froth inline steam injection processing |
US20050209495A1 (en) * | 2004-03-22 | 2005-09-22 | Mccoy James N | Process for steam cracking heavy hydrocarbon feedstocks |
US20050261533A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Cracking hydrocarbon feedstock containing resid utilizing partial condensation of vapor phase from vapor/liquid separation to mitigate fouling in a flash/separation vessel |
US20050261531A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid |
US20050261534A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and draft control system for use in cracking a heavy hydrocarbon feedstock in a pyrolysis furnace |
US20050261532A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids |
US20050261538A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Process for reducing vapor condensation in flash/separation apparatus overhead during steam cracking of hydrocarbon feedstocks |
US20050261536A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Apparatus and process for controlling temperature of heated feed directed to a flash drum whose overhead provides feed for cracking |
US20050261535A1 (en) * | 2004-05-21 | 2005-11-24 | David Beattie | Steam cracking of light hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20050261537A1 (en) * | 2004-05-21 | 2005-11-24 | Stell Richard C | Steam cracking of hydrocarbon feedstocks containing non-volatile components and/or coke precursors |
US20060006556A1 (en) * | 2004-07-08 | 2006-01-12 | Chen Hung Y | Gas supply device by gasifying burnable liquid |
US20060014994A1 (en) * | 2004-07-16 | 2006-01-19 | Keusenkothen Paul F | Reduction of total sulfur in crude and condensate cracking |
US20060014993A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20060014992A1 (en) * | 2004-07-14 | 2006-01-19 | Stell Richard C | Process for reducing fouling from flash/separation apparatus during cracking of hydrocarbon feedstocks |
US20060089519A1 (en) * | 2004-05-21 | 2006-04-27 | Stell Richard C | Process and apparatus for cracking hydrocarbon feedstock containing resid to improve vapor yield from vapor/liquid separation |
US20060094918A1 (en) * | 2004-10-28 | 2006-05-04 | Mccoy James N | Steam cracking of hydrocarbon feedstocks containing salt and/or particulate matter |
US20060129012A1 (en) * | 2004-12-10 | 2006-06-15 | Frye James M | Vapor/liquid separation apparatus |
US7090765B2 (en) | 2002-07-03 | 2006-08-15 | Exxonmobil Chemical Patents Inc. | Process for cracking hydrocarbon feed with water substitution |
US20060231456A1 (en) * | 2005-04-11 | 2006-10-19 | Bhan Opinder K | Systems, methods, and catalysts for producing a crude product |
US20060234877A1 (en) * | 2005-04-11 | 2006-10-19 | Bhan Opinder K | Systems, methods, and catalysts for producing a crude product |
US20060231457A1 (en) * | 2005-04-11 | 2006-10-19 | Bhan Opinder K | Systems, methods, and catalysts for producing a crude product |
US20060249430A1 (en) * | 2005-04-06 | 2006-11-09 | Mesters Carolus Matthias A M | Process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock |
US20060289340A1 (en) * | 2003-12-19 | 2006-12-28 | Brownscombe Thomas F | Methods for producing a total product in the presence of sulfur |
US20070004952A1 (en) * | 2005-06-30 | 2007-01-04 | Mccoy James N | Steam cracking of partially desalted hydrocarbon feedstocks |
US20070000810A1 (en) * | 2003-12-19 | 2007-01-04 | Bhan Opinder K | Method for producing a crude product with reduced tan |
US20070000808A1 (en) * | 2003-12-19 | 2007-01-04 | Bhan Opinder K | Method and catalyst for producing a crude product having selected properties |
US20070000811A1 (en) * | 2003-12-19 | 2007-01-04 | Bhan Opinder K | Method and catalyst for producing a crude product with minimal hydrogen uptake |
US20070012595A1 (en) * | 2003-12-19 | 2007-01-18 | Brownscombe Thomas F | Methods for producing a total product in the presence of sulfur |
WO2007071177A1 (fr) * | 2005-12-23 | 2007-06-28 | China Petroleum & Chemical Corporation | Methode de conversion catalytique destinee a augmenter le rendement d'olefines inferieures |
US20070215524A1 (en) * | 2004-05-21 | 2007-09-20 | Stell Richard C | Vapor/liquid separation apparatus for use in cracking hydrocarbon feedstock containing resid |
US20070295646A1 (en) * | 2006-06-22 | 2007-12-27 | Bhan Opinder K | Method for producing a crude product with a long-life catalyst |
US20070295647A1 (en) * | 2006-06-22 | 2007-12-27 | Brownscombe Thomas F | Methods for producing a total product with selective hydrocarbon production |
US20070295645A1 (en) * | 2006-06-22 | 2007-12-27 | Brownscombe Thomas F | Methods for producing a crude product from selected feed |
US20080083655A1 (en) * | 2006-10-06 | 2008-04-10 | Bhan Opinder K | Methods of producing a crude product |
US20080110801A1 (en) * | 2006-11-09 | 2008-05-15 | Leon Yuan | Process For Heating A Hydrocarbon Stream Entering A Reaction Zone With A Heater Convection Section |
US20090152172A1 (en) * | 2006-05-10 | 2009-06-18 | United Technologies Corporation | In-situ continuous coke deposit removal by catalytic steam gasification |
US7740751B2 (en) | 2006-11-09 | 2010-06-22 | Uop Llc | Process for heating a stream for a hydrocarbon conversion process |
US20100243521A1 (en) * | 2009-03-31 | 2010-09-30 | Peters Kenneth D | Fired Heater for a Hydrocarbon Conversion Process |
US7918992B2 (en) | 2005-04-11 | 2011-04-05 | Shell Oil Company | Systems, methods, and catalysts for producing a crude product |
US20110295051A1 (en) * | 2010-05-31 | 2011-12-01 | Wang Shizhong | Method and reactor for cracking hydrocarbon |
WO2012161873A1 (en) * | 2011-05-20 | 2012-11-29 | Exxonmobil Chemical Patents Inc. | Coke gasification on catalytically active surfaces |
US20130184510A1 (en) * | 2012-01-13 | 2013-07-18 | United Technologies Corporation | Method for reducing coke deposition |
US20130267750A1 (en) * | 2010-12-22 | 2013-10-10 | General Electric Company | Method and reactor for cracking hydrocarbon and method for coating the reactor |
US20140120007A1 (en) * | 2012-10-26 | 2014-05-01 | Modine Mfg. Co. | Reactor core for use in a chemical reactor, and method of making the same |
Families Citing this family (1)
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---|---|---|---|---|
DE102011107933A1 (de) | 2011-07-19 | 2013-01-24 | Thyssenkrupp Uhde Gmbh | Prozessintensivierung von Dampfreformern durch Verwendung angepasster Katalysatoren |
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-
1996
- 1996-01-10 DE DE19600684A patent/DE19600684A1/de not_active Withdrawn
- 1996-01-29 AR ARP960101190A patent/AR000827A1/es unknown
- 1996-02-14 DE DE59605560T patent/DE59605560D1/de not_active Expired - Fee Related
-
2002
- 2002-10-22 US US10/274,987 patent/US20030070963A1/en not_active Abandoned
Patent Citations (4)
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US4427721A (en) * | 1977-11-01 | 1984-01-24 | United Kingdom Atomic Energy Authority | Method of coating steel substrates to reduce carbonaceous deposition thereon |
US4361478A (en) * | 1978-12-14 | 1982-11-30 | Linde Aktiengesellschaft | Method of preheating hydrocarbons for thermal cracking |
US4599480A (en) * | 1985-07-12 | 1986-07-08 | Shell Oil Company | Sequential cracking of hydrocarbons |
US5658452A (en) * | 1994-01-04 | 1997-08-19 | Chevron Chemical Company | Increasing production in hydrocarbon conversion processes |
Cited By (193)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040004028A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Converting mist flow to annular flow in thermal cracking application |
US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
US7578929B2 (en) | 2002-07-03 | 2009-08-25 | Exxonmoil Chemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US7138047B2 (en) | 2002-07-03 | 2006-11-21 | Exxonmobil Chemical Patents Inc. | Process for steam cracking heavy hydrocarbon feedstocks |
US7097758B2 (en) | 2002-07-03 | 2006-08-29 | Exxonmobil Chemical Patents Inc. | Converting mist flow to annular flow in thermal cracking application |
US7090765B2 (en) | 2002-07-03 | 2006-08-15 | Exxonmobil Chemical Patents Inc. | Process for cracking hydrocarbon feed with water substitution |
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Also Published As
Publication number | Publication date |
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AR000827A1 (es) | 1997-08-06 |
DE59605560D1 (de) | 2000-08-17 |
DE19600684A1 (de) | 1996-08-22 |
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